CN108299634B - Production system and production method of multi-type polyester intermediates - Google Patents
Production system and production method of multi-type polyester intermediates Download PDFInfo
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- CN108299634B CN108299634B CN201810080129.6A CN201810080129A CN108299634B CN 108299634 B CN108299634 B CN 108299634B CN 201810080129 A CN201810080129 A CN 201810080129A CN 108299634 B CN108299634 B CN 108299634B
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/66—Polyesters containing oxygen in the form of ether groups
- C08G63/668—Polyesters containing oxygen in the form of ether groups derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/672—Dicarboxylic acids and dihydroxy compounds
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/82—Preparation processes characterised by the catalyst used
- C08G63/85—Germanium, tin, lead, arsenic, antimony, bismuth, titanium, zirconium, hafnium, vanadium, niobium, tantalum, or compounds thereof
- C08G63/86—Germanium, antimony, or compounds thereof
- C08G63/866—Antimony or compounds thereof
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Abstract
The invention discloses a production system and a production method of multi-type polyester intermediates. The system prepares different slurry materials by a slurry preparation tank I and a slurry preparation tank II, the slurry materials pass through a first-stage esterification reaction kettle and then are respectively divided into two paths to a first-line/second-line second-stage esterification reaction kettle, a first-line/second-line pre-polycondensation reaction kettle and a first-line/second-line final-polycondensation reaction kettle, and bottle-grade polyester products and hot pot polyester product basic slices are respectively prepared by controlling a valve, a flowmeter and process parameters. The system can be used for simultaneously preparing products with different requirements without changing the production requirements of the prepared products, thereby reducing the raw material waste caused by a large amount of transition materials generated by the production change and the influence of the generated waste materials on the environment; the system is simple to operate, safe and easy to implement, saves raw materials, reduces production cost and has better social and economic benefits.
Description
Technical Field
The invention belongs to the technical field of polyester production, and relates to a production system and a production method of various polyester intermediates, namely, various polyester basic slices can be produced simultaneously by adopting the system.
Technical Field
Polyesters, polymer assemblies obtained by polycondensation of polyols and polyacids. The polyester is an engineering plastic with excellent performance and wide application, and is widely applied to the fields of packaging industry, electronic and electric appliances, medical treatment and health, buildings, automobiles and the like. Therefore, with the rapid development of Chinese economy, the apparent consumption of the polyester in China is rapidly increased, and meanwhile, the polyester production capacity is rapidly developed.
While polyester is rapidly developed, its preparation process is also rapidly developed. Most of the existing polyester production processes are produced in a mode of one end and two ends, raw materials and auxiliary materials, namely Purified Terephthalic Acid (PTA), ethylene glycol, isophthalic acid (IPA), a catalyst and an additive are metered and added into a slurry preparation tank according to a certain proportion to form slurry in the production process, the slurry is conveyed to a first-stage esterification system, namely, the esterification rate is improved, then the slurry enters a second-stage esterification system through two paths respectively, and different types of polyester chips are produced through product indexes controlled by pre-polycondensation and final polycondensation. In the production process, because the hot pot polyester product cannot be prepared due to the addition of IPA, only water bottles, oil bottles and carbonic acid-grade products can be produced, so that the whole system needs to be converted to production for preparing the hot pot polyester product (without the addition of IPA) when the hot pot polyester product needs to be prepared, a large amount of transition materials are generated in the conversion process to become waste materials, the waste of raw materials is caused, and the production cost is also increased.
Disclosure of Invention
In order to solve the problems, the invention provides a production system of various polyester intermediates and a method for producing polyester products by adopting the system, the system can be used for producing water bottles, oil bottles or basic slices of carbonic acid-grade products without transferring production, and can also be used for producing basic slices of hot-pot polyester; the basic slices of two polyester products can be produced simultaneously, so that the production efficiency is obviously improved, and the waste of raw materials is reduced; the system is simple to operate, safe and easy to operate.
The invention is realized by the following technical scheme
A production system of multiple types of polyester intermediates comprises a slurry preparation tank I, wherein the slurry preparation tank I is communicated with a slurry delivery pump through a material delivery pipeline, the slurry delivery pump is communicated with a feed inlet of a primary esterification reaction kettle through a material delivery pipeline A, a first discharge port of the primary esterification reaction kettle is communicated with a three-way pipe joint through a material delivery pipeline, and two material delivery pipelines, namely a material delivery pipeline branch pipe B and a material delivery pipeline branch pipe C, are led out from the three-way pipe joint; the material conveying pipeline branch pipe B is communicated with a first feeding hole of the first-line second-stage esterification reaction kettle, a discharging hole of the first-line second-stage esterification reaction kettle is communicated with a feeding hole of the first-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the first-line pre-polycondensation reactor is communicated with a feeding hole of the first-line final-polycondensation reactor through a material conveying pipeline; the material conveying pipeline branch pipe C is communicated with a first feeding hole of the second-line diester reaction kettle, a discharging hole of the second-line second-stage esterification reaction kettle is communicated with a feeding hole of the second-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the second-line pre-polycondensation reactor is communicated with a feeding hole of the second-line final polycondensation reactor through a material conveying pipeline;
the system also comprises a slurry preparation tank II, wherein the bottom of the slurry preparation tank II is provided with a first discharge hole and a second discharge hole; a first discharge hole at the bottom of the slurry configuration groove II is communicated with a first slurry delivery pump through a material delivery pipeline, the first slurry delivery pump is communicated with a first flow regulating valve through a material delivery pipeline D, and the first flow regulating valve is communicated with a second feed hole of the first-line second-stage esterification reaction kettle through a material delivery pipeline E; and a second discharge port at the bottom of the slurry configuration groove II is communicated with a second slurry delivery pump through a material delivery pipeline, the second slurry delivery pump is communicated with a second flow regulating valve through a material delivery pipeline F, and the second flow regulating valve is communicated with a second feed port of the second-line second-stage esterification reaction kettle through a material delivery pipeline G.
In the production system of the multiple types of polyester intermediates, the material conveying pipeline A is provided with a flowmeter A and a three-way valve, and the three-way valve is communicated with a feed inlet of the slurry preparation tank I through a backflow pipeline; valves are arranged on the material conveying pipeline B and the material conveying pipeline C; the valve is an automatic control valve.
In the production system of the various polyester intermediates, the material conveying pipeline D is provided with a three-way valve a, and the three-way valve a is communicated with the ethylene glycol storage device through a first flushing pipeline; and the material conveying pipeline M is provided with a three-way valve b, and the three-way valve b is communicated with the ethylene glycol storage device through a second flushing pipeline.
In the production system of the multi-type polyester intermediates, a first check valve, a three-way valve c and a three-way valve E are sequentially arranged on the material conveying pipeline E from a first slurry conveying pump to a first flow regulating valve; a second check valve, a three-way valve d and a three-way valve f are sequentially arranged on the material conveying pipeline N from the second slurry conveying pump to the second flow regulating valve; the three-way valve c is communicated with the three-way valve d through a material conveying pipeline S, and the three-way valve e is communicated with the three-way valve f through a material conveying pipeline T; the material conveying pipeline S is provided with a three-way valve g, the material conveying pipeline T is provided with a three-way valve h, and the three-way valve g is communicated with the three-way valve h through a material conveying pipeline Q (a flow meter is arranged between a first slurry conveying pump and a first check valve on the material conveying pipeline E, and a flow meter is arranged between a second slurry conveying pump and a second check valve on the material conveying pipeline N).
The production system of multiple type of polyester midbody, material conveying pipeline Q on be equipped with thick liquids flowmeter and valve.
In the production system of the multi-type polyester intermediates, the material conveying pipeline F is provided with a three-way valve j, the three-way valve j is communicated with the ethylene glycol storage device through a flushing pipeline, and the three-way valve j is also communicated with a feed inlet of the slurry preparation tank II through a backflow pipeline; the material conveying pipeline P is provided with a three-way valve k, the three-way valve k is communicated with the ethylene glycol storage device through a flushing pipeline, and the three-way valve k is communicated with a feeding hole of the slurry configuration groove II through a backflow pipeline (a pressure gauge is arranged between a first flow regulating valve and a three-way valve j on the material conveying pipeline F, and a pressure gauge is arranged between a second flow regulating valve and the three-way valve k on the material conveying pipeline P).
A method for producing a plurality of kinds of polyester intermediates using the above production system for a plurality of kinds of polyester intermediates, comprising the steps of:
(1) preparing the required raw materials of PTA, IPA, ethylene glycol, a catalyst, an erythroid solution, a blue agent solution and diethylene glycol;
(2) adding the material prepared in the step (1) into a slurry preparation tank I, and stirring, wherein the components and the mass percentage of each component in the slurry preparation tank I are as follows, PTA: 68-69%, ethylene glycol: 27-29%, catalyst: 1.2-1.3%, and a redness agent solution: 0.3-0.4%, bluing agent solution: 0.15 to 0.19%, diethylene glycol: 0.4-0.5% of the raw materials are mixed and stirred uniformly; simultaneously, IPA and glycol are added into the slurry preparation tank II and are uniformly stirred, the mass percent of IPA in the slurry preparation tank II is 50%, and the mass percent of glycol is 50%; the materials in the slurry preparation tank I and the slurry preparation tank II are uniformly mixed and stirred;
(3) after the mixture obtained in the step (2) is uniformly mixed and stirred, the mixture obtained in the slurry preparation tank I is conveyed to a slurry conveying pump from a discharge port at the lower end of the slurry stirring tank I through a material conveying pipeline, conveyed to a first feed port of the primary esterification reaction kettle through a material conveying pipeline A under the action of the conveying pump, and added into the primary esterification reaction kettle;
the flow rate of the materials in the slurry preparation tank I when the materials are added into the primary esterification reaction kettle is 26000-48000 kg/h; after adding, carrying out reaction in a first-stage esterification reaction kettle, wherein the reaction temperature is 250-265 ℃, the reaction time is 4-5.5 h, and the reaction pressure is 60-70 KPa; after the first-stage esterification reaction is finished, obtaining a material of the first-stage esterification reaction;
(4) respectively conveying the materials of the primary esterification reaction obtained in the step (3) to a material conveying pipeline branch pipe B and a material conveying pipeline branch pipe C through a three-way pipe joint;
then the material of the first-stage esterification reaction is conveyed to a first feed inlet of the first-line second-stage esterification reaction by a material conveying pipeline branch pipe B and added into a first-line second-stage esterification reaction kettle to carry out the second-stage esterification reaction; in the process, the flow of the material conveying pipeline branch pipe B conveyed into the first-line second-stage esterification reaction kettle is 11000-21000 kg/h; after the addition, the reaction time in the first-line second-stage esterification reaction kettle is 1.2-1.5 h, the reaction temperature is 255-270 ℃, and the reaction pressure is 3-8 KPa; after the reaction is finished, a first-line secondary esterification reaction material is obtained;
meanwhile, the material of the first-stage esterification reaction is conveyed to a first feed port of the second-line second-stage esterification reaction kettle through a material conveying pipeline branch pipe C and added into the second-line second-stage esterification reaction kettle, and meanwhile, the mixed material in the slurry configuration tank II is conveyed to a second feed port of the second-line second-stage esterification reaction kettle through a first slurry conveying pump and added into the second-line second-stage esterification reaction kettle, and is mixed with the material added from the first feed port to carry out second-stage esterification reaction; in the process, the flow of the material when the material is added into the first charging opening of the two-line two-stage esterification reaction kettle through the material conveying pipeline branch pipe C is as follows: 11000 to 21000kg/h, wherein the flow rate of the mixed material in the slurry preparation tank II when the mixed material is added through a second feed inlet of the second-line secondary esterification reaction kettle is 850 kg/h; after the materials are added, the reaction time in the second-line second-stage esterification reaction kettle is 1.2-1.5 h, the reaction temperature is 255-270 ℃, and the reaction pressure is 3-8 KPa; after the reaction is finished, a material of the second-line second-stage esterification reaction is obtained;
(5) discharging a first-line second-stage esterification reaction material obtained after the esterification reaction in the first-line second-stage esterification reaction kettle in the step (4) from a discharge hole at the bottom of the reaction kettle, conveying the material to a first-line pre-polycondensation reactor through a material conveying pipeline, and carrying out pre-polycondensation reaction; the reaction time of the pre-polycondensation reaction in the first-line pre-polycondensation reactor is 2-2.5 h, the upper chamber temperature of the reaction is 265-275 ℃, the lower chamber temperature is 270-276 ℃, the upper chamber pressure of the reaction is 7-10 KPa (a), and the lower chamber pressure is 1.1-1.2 KPa (a); discharging a pre-polycondensation product obtained after the pre-polycondensation reaction is finished through a discharge port of the pre-polycondensation reactor, and conveying the pre-polycondensation product to a first-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction; carrying out a final polycondensation reaction in a first-line final polycondensation reactor for 1.5-2.5 h, at a reaction temperature of 278-285 ℃ and a reaction pressure of 120-250 KPa (a), and obtaining a basic slice of a hot tank grade polyester product after the reaction is finished; (the obtained intermediate is the intermediate of the hot tank grade polyester product, and the obtained hot tank polyester basic slice can be prepared into the final polyester product by adopting the conventional method and the preparation of a solid phase device.)
Discharging a second-line second-stage esterification reaction material obtained after the esterification reaction in the second-line second-stage esterification reaction kettle in the step (4) from a discharge hole at the bottom of the second-line second-stage esterification reaction kettle, conveying the material to a second-line pre-polycondensation reactor through a material conveying pipeline, and reacting; the reaction time of the reaction in the second-line pre-polycondensation reactor is 2-2.5 h, the upper chamber temperature of the reaction is 265-275 ℃, the lower chamber temperature of the reaction is 270-276 ℃, the upper chamber pressure of the reaction is 7-10 KPa (a), the lower chamber pressure is 1.1-1.2 KPa (a), the pre-polycondensation product obtained after the second-line pre-polycondensation reaction is finished is discharged from a discharge port of the pre-polycondensation reactor, and then is conveyed into the second-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction; the reaction time is 1.5-2.5 h, the reaction temperature is 278-285 ℃, the reaction pressure is 120-250 KPa (a) when the reaction is carried out in the second-line final polycondensation reactor, and a basic slice of a bottle-grade polyester product is obtained after the reaction is finished; (namely the obtained intermediate of the bottle-grade polyester product, and the obtained basic slice of the bottle-grade polyester product can be prepared into the final polyester product by a common method through the preparation of a solid phase device).
The method for producing various polyester intermediates by using the production system for various polyester intermediates, further comprising the following steps: and (3) after the material after the first-stage esterification reaction in the step (4) is conveyed to the first-line second-stage esterification reaction kettle through the material conveying pipeline branch pipe B, the mixture in the slurry preparation tank II is also added into the first-line second-stage esterification reaction kettle through the first slurry conveying pump to be mixed with the material after the first-stage esterification reaction for second-stage esterification reaction, and after the second-stage esterification reaction, pre-polycondensation reaction and final polycondensation reaction are sequentially carried out to obtain a basic slice of a bottle-grade polyester product (and then the final polyester product can be prepared by adopting a common method through a solid phase device).
The method for producing various polyester intermediates by using the production system for various polyester intermediates, further comprising the following steps: and (3) conveying the material subjected to the first-stage esterification reaction to a second-line second-stage esterification reaction kettle through a material conveying pipeline branch pipe C, then performing second-stage esterification reaction (namely, no IPA mixed material in a slurry preparation tank II is added), after the second-stage esterification reaction is finished, sequentially conveying the material to a second-line pre-polycondensation reactor and a second-line final polycondensation reactor through a material conveying pipeline to perform pre-polycondensation and final polycondensation reaction, and after the final polycondensation reaction is finished, obtaining a basic slice of a hot tank-grade polyester product (and then preparing the final polyester product through a solid phase device by adopting a common method).
The method for producing various polyester intermediates by adopting the production system of various polyester intermediates comprises the steps that the catalyst in the step (1) is ethylene glycol antimony; the mass concentration of the redness agent in the redness agent solution is 160 PPM; the mass concentration of the blueness agent in the blueness agent solution is 800 PPM.
Compared with the prior art, the invention has the following positive and beneficial effects
The production system can simultaneously produce bottle-grade polyester and hot tank-grade polyester, also can produce single polyester in large batch, and can flexibly adjust the variety of the produced product according to market demands; the production can be carried out simultaneously no matter bottle-grade polyester products or hot tank-grade polyester products are needed, the system does not need to carry out production conversion, and a large amount of waste of raw materials, waste materials and manpower and material resources input due to waste material recovery in the production conversion process are reduced; the influence of the generation of waste on the environment is also reduced;
therefore, the production process greatly improves the production efficiency, meets the requirements of various polyester products, does not cause the waste of raw materials and the generation of a large amount of waste materials, reduces the production cost, saves manpower and material resources and has good social and economic benefits;
the production system is provided with a plurality of backflow pipelines, so that the raw materials can be fully and efficiently utilized, the utilization rate of the raw materials is improved, the waste of the raw materials is further reduced, and the production cost is reduced;
the production system and the production process are simple and easy to operate, accurate to control and safe to operate.
Drawings
FIG. 1 shows one of the schematic diagrams of production systems of various kinds of polyester intermediates,
FIG. 2 shows a second schematic diagram of a production system for various polyester intermediates,
FIG. 3 shows a third schematic diagram of a production system for various polyester-like intermediates,
the symbols in the drawings indicate that: 1 represents a slurry preparation tank I, 101 represents a first feed inlet of the slurry preparation tank I, 102 represents a second feed inlet of the slurry preparation tank, 2 represents a slurry delivery pump, 3 represents a material delivery pipeline A, 4 represents a first-stage esterification reaction kettle, 401 represents a first discharge outlet of the first-stage esterification reaction kettle, 5 represents a three-way pipe joint, 6 represents a material delivery pipeline branch pipe B, 601 represents a valve B, 7 represents a first-line second-stage esterification reaction kettle, 701 represents a first feed inlet of the first-line second-stage esterification reaction kettle, 702 represents a second feed inlet of the first-line second-stage esterification reaction kettle, 8 represents a first-line pre-polycondensation reactor, 9 represents a first-line final polycondensation reactor, 10 represents a material delivery pipeline branch pipe C, 1001 represents a valve C, 11 represents a second-line second-stage esterification reaction kettle, 1101 represents a first feed inlet of the second-line second-stage esterification reaction kettle, 1102 represents a second feed inlet of the second-line, 12 denotes a second-line prepolycondensation reactor, 13 denotes a second-line finisher;
14 denotes a slurry preparation tank ii, 15 denotes a first discharge port of the slurry preparation tank ii, 16 denotes a material transport line D, 1601 denotes a three-way valve a, 1602 denotes a first flush line, 17 denotes a first slurry transport pump, 18 denotes a material transport line E, 19 denotes a first flow rate adjustment valve, 20 denotes a material transport line F, 21 denotes a second discharge port of the slurry preparation tank ii, 22 denotes a material transport line M, 2201 denotes a three-way valve b, 2202 denotes a second flush line, 23 denotes a second slurry transport pump, 24 denotes a material transport line N, 25 denotes a second flow rate adjustment valve, and 26 denotes a material transport line P; 27 denotes a first check valve, 28 denotes a three-way valve c, 29 denotes a three-way valve e, 30 denotes a second check valve, 31 denotes a three-way valve d, 32 denotes a three-way valve f, 33 denotes a material transport conduit S, 34 denotes a material transport conduit T, 35 denotes a three-way valve g, 36 denotes a three-way valve h, 37 denotes a material transport conduit Q, 38 denotes a slurry flow meter;
39 denotes a return line, 40 denotes a three-way valve j, 41 denotes a third flushing line, 42 denotes a first return line, 43 denotes a three-way valve k, 44 denotes a fourth flushing line, 45 denotes a second return line, and 46 denotes a return feed opening of the slurry preparation tank ii.
Detailed Description
The present invention will be described in more detail with reference to the following embodiments, but the present invention is not limited to the embodiments.
Example 1
A production system of multiple types of polyester intermediates is shown in figure 1 and comprises a slurry preparation tank I, wherein the slurry preparation tank I is communicated with a slurry delivery pump through a material delivery pipeline, the slurry delivery pump is communicated with a feed inlet of a first-stage esterification reaction kettle through a material delivery pipeline A, a first discharge outlet of the first-stage esterification reaction kettle is communicated with a three-way pipe joint through a material delivery pipeline, and two material delivery pipeline branch pipes, namely a material delivery pipeline branch pipe B and a material delivery pipeline branch pipe C, are led out from the three-way pipe joint; the material conveying pipeline branch pipe B is communicated with a first feeding hole of the first-line second-stage esterification reaction kettle, a discharging hole of the first-line second-stage esterification reaction kettle is communicated with a feeding hole of the first-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the first-line pre-polycondensation reactor is communicated with a feeding hole of the first-line final-polycondensation reactor through a material conveying pipeline; the material conveying pipeline branch pipe C is communicated with a first feeding hole of the second-line second-stage esterification reaction kettle, a discharging hole of the second-line second-stage esterification reaction kettle is communicated with a feeding hole of the second-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the second-line pre-polycondensation reactor is communicated with a feeding hole of the second-line final-polycondensation reactor through a material conveying pipeline;
the system also comprises a slurry preparation tank II, wherein the bottom of the slurry preparation tank II is provided with a first discharge hole and a second discharge hole; a first discharge hole at the bottom of the slurry preparation tank II is communicated with a first slurry conveying pump through a material conveying pipeline D, the first slurry conveying pump is communicated with a first flow regulating valve through a material conveying pipeline E, and the first flow regulating valve is communicated with a second feed hole of the first-line second-stage esterification reaction kettle through a material conveying pipeline F; and a second discharge port at the bottom of the slurry preparation tank II is communicated with a second slurry delivery pump through a material delivery pipeline M, the second slurry delivery pump is communicated with a second flow regulating valve through a material delivery pipeline N, and the second flow regulating valve is communicated with a second feed port of the second-line second-stage esterification reaction kettle through a material delivery pipeline P.
Further, a flowmeter A and a three-way valve are arranged on the material conveying pipeline A; and the material conveying pipeline branch pipe B and the material conveying pipeline branch pipe C are respectively provided with an automatic control valve.
Further, a three-way valve a is arranged on the material conveying pipeline D and communicated with the ethylene glycol storage device through a first flushing pipeline; and the material conveying pipeline M is provided with a three-way valve b, and the three-way valve b is communicated with the ethylene glycol storage device through a second flushing pipeline.
Example 2
On the basis of the above embodiment 1, the same components in fig. 2 as those in fig. 1 have the same functions, and detailed descriptions of these components are omitted for the sake of brevity.
As shown in fig. 2, the system further includes: the material conveying pipeline E is sequentially provided with a first check valve, a three-way valve c and a three-way valve E from a first slurry conveying pump to a first flow regulating valve; the material conveying pipeline N is sequentially provided with a second check valve, a three-way valve d and a three-way valve f from a second slurry conveying pump to a second flow regulating valve; the three-way valve c is communicated with the three-way valve d through a material conveying pipeline S, and the three-way valve e is communicated with the three-way valve f through a material conveying pipeline T; the material conveying pipeline S is provided with a three-way valve g, the material conveying pipeline T is provided with a three-way valve h, and the three-way valve g is communicated with the three-way valve h through a material conveying pipeline Q;
furthermore, a slurry flow meter and an automatic control valve are arranged on the material conveying pipeline Q.
Example 3
On the basis of the above embodiments 1 and 2, the same components in fig. 3 as those in fig. 1 and 2 have the same functions, and detailed descriptions of these components are omitted for the sake of brevity.
As shown in fig. 3, the three-way valve on the material conveying pipeline a is communicated with the feed inlet of the slurry preparation tank i through a return pipeline;
the material conveying pipeline F is provided with a three-way valve j, the three-way valve j is communicated with the ethylene glycol storage device through a third flushing pipeline, and the three-way valve j is also communicated with a feeding hole of the slurry preparation tank II through a first backflow pipeline; and the material conveying pipeline P is provided with a three-way valve k, the three-way valve k is communicated with the ethylene glycol storage device through a fourth flushing pipeline, and the three-way valve k is communicated with a feeding hole of the slurry preparation tank II through a second backflow pipeline.
Example 4
A method for producing a plurality of kinds of polyester intermediates using the above-mentioned production system for a plurality of kinds of polyester intermediates, comprising the steps of:
(1) preparing required raw materials: pure Terephthalic Acid (PTA), isophthalic acid (IPA), ethylene glycol antimony, a reddish agent solution with the mass concentration of 160ppm, a bluish agent solution with the mass concentration of 800ppm, and diethylene glycol;
(2) adding Purified Terephthalic Acid (PTA), ethylene glycol antimony, 160ppm by mass of a red agent solution, 800ppm by mass of a blue agent solution and diethylene glycol into the raw materials prepared in the step (1), mixing and stirring the raw materials in a slurry preparation tank I, wherein the mass percentages of the components are as follows: PTA: 68-69%, ethylene glycol: 27-29%, ethylene glycol antimony: 1.2-1.3%, and a redness agent solution: 0.3-0.4%, bluing agent solution: 0.15 to 0.19%, diethylene glycol: 0.4-0.5%, and uniformly mixing and stirring;
and (2) adding the isophthalic acid (IPA) and the ethylene glycol prepared in the step (1) into a slurry preparation tank II, and mixing and stirring, wherein the slurry preparation tank II comprises the following components in percentage by mass: IPA: 50%, ethylene glycol: 50 percent, mixing and stirring evenly; (3) uniformly stirring the mixture in the slurry preparation tank I and the slurry preparation tank II in the step (2);
discharging the mixture in the slurry preparation tank I from a discharge port at the lower end of the slurry preparation tank I, conveying the mixture to a slurry conveying pump through a material conveying pipeline, conveying the mixture to a first feed port of a first-stage esterification reaction kettle through a material conveying pipeline A under the action of the slurry conveying pump, and adding the mixture into the first-stage esterification reaction kettle; wherein the flow rate of the mixture when the mixture is added into a first-stage esterification reaction kettle is 45000-48000 kg/h, the mixture is added into the first-stage esterification reaction kettle to react, the temperature during the reaction is 263 +/-2 ℃, the pressure during the reaction is 60-70 KPa, and the reaction time is 4-5 hours, (the liquid level in the first-stage esterification reaction kettle is (75 +/-1)%), and the material of the first-stage esterification reaction is obtained after the reaction is finished;
(4) conveying the material obtained in the step (3) after the primary esterification reaction to a three-way pipe joint through a material conveying pipeline, and then respectively conveying the material to a material conveying pipeline branch pipe B and a material conveying pipeline branch pipe C through the three-way pipe joint;
the material of the first-stage esterification reaction in the material conveying pipeline branch pipe B is added into the first-stage second-stage esterification reaction kettle through a first feed inlet of the first-stage second-stage esterification reaction kettle to carry out the first-stage second-stage esterification reaction; in the process, the adding force of the material of the first-stage esterification reaction in the material conveying pipeline branch pipe B when being added into the first-line second-stage esterification reaction kettle is 19000-21000 kg/h; after the addition, the temperature for reaction in a first-line secondary esterification reaction kettle is 266 +/-2 ℃, the pressure for reaction is 3-8 KPa, and the reaction time is 1.2-1.5 hours, (the liquid level in the first-line secondary esterification reaction kettle is (65 +/-1)%), and the first-line secondary esterification reaction material is obtained after the reaction is finished;
meanwhile, the material of the first-stage esterification reaction in the material conveying pipeline branch pipe C is added into the second-line second-stage esterification reaction kettle through a first feed port of the second-line second-stage esterification reaction kettle, and the mixture in the slurry preparation tank II is also added into the second-line second-stage esterification reaction kettle through a second feed port of the second-line second-stage esterification reaction kettle through a first slurry conveying pump and is mixed with the material of the first-stage esterification reaction for second-stage esterification reaction; in the process, the flow rate of the material of the first-order esterification reaction in the material conveying pipeline branch pipe C is 19000-21000 kg/h when the material is added into the second-order esterification reaction kettle through the first feed port of the second-order esterification reaction kettle, and the flow rate of the mixture in the slurry preparation tank II is 750-850 kg/h when the mixture is added into the second-order esterification reaction kettle through the material conveying pipeline from the second feed port of the second-order esterification reaction kettle; after the addition is finished, carrying out reaction in a second-line secondary esterification reaction kettle, wherein the reaction temperature is 266 +/-2 ℃, the pressure is 3-8 KPa and the reaction time is 1.2-1.5 h, (the liquid level in the second-line secondary esterification reaction kettle is (65 +/-1)%); after the reaction is finished, a material of the second-line second-stage esterification reaction is obtained;
(5) discharging a material of the first-line second-stage esterification reaction obtained after the esterification reaction in the first-line second-stage esterification reaction kettle in the step (4) from a discharge port at the bottom of the reaction kettle, conveying the material to a first-line pre-polycondensation reactor through a material conveying pipeline for pre-polycondensation reaction, wherein the upper chamber temperature of the first-line pre-polycondensation reactor is 273 +/-0.5 ℃, the upper chamber pressure is 7-10 KPa (a), the lower chamber temperature of the first-line pre-polycondensation reactor is 275 +/-0.5 ℃, the lower chamber pressure of the first-line pre-polycondensation reactor is 1.1-1.2 KPa (a), the reaction time is 2-2.5 hours, (the liquid level of the upper chamber is 25% and the liquid level of the lower chamber is 50%) in the first-line second-stage pre-; conveying a first-line pre-polycondensation product obtained after the reaction to a first-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction, wherein the temperature and the pressure during the reaction in the first-line final polycondensation reactor are 278-285 ℃, 120-250 KPa (a), and the reaction time is 1.5-2.0 hours, (the liquid level during the first-line final polycondensation reaction is (25 +/-2)%), and obtaining a basic slice of the hot tank grade polyester after the reaction is finished (the basic slice of the hot tank grade polyester product is an intermediate of the hot tank grade polyester product, and the obtained basic slice of the hot tank grade polyester product can be prepared into a final polyester product through a common method and a preparation device;
discharging a second-line second-stage esterification reaction material obtained after the esterification reaction in the second-line second-stage esterification reaction kettle in the step (4) from a discharge port at the bottom of the second-line second-stage esterification reaction kettle, conveying the second-line second-stage esterification reaction material to a second-line pre-polycondensation reactor for reaction through a material conveying pipeline, wherein the upper chamber temperature and the upper chamber pressure are 273 +/-0.5 ℃ and 7-10 KPa (a) respectively, the lower chamber temperature and the lower chamber pressure are 275 +/-0.5 ℃ and 1.1-1.2 KPa (a) respectively, the reaction time is 2-2.5 hours, (the liquid level of the upper chamber is 25% and the liquid level of the lower chamber is 50% respectively) in the second-line second-stage pre-polycondensation reaction process; discharging the second-line pre-polycondensation product obtained after the reaction through a discharge hole of a second-line pre-polycondensation reactor, conveying the second-line pre-polycondensation product to the second-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction, wherein the temperature in the final polycondensation reaction is 278-285 ℃, the reaction pressure is 120-250 KPa (a), and the reaction time is 1.5-2 hours, (the liquid level in the second-line final polycondensation reaction process is (25 +/-2)%), and obtaining a base slice of a bottle-grade polyester product after the reaction is finished (the base slice of the bottle-grade polyester product is an intermediate of the bottle-grade polyester product, and the base slice of the bottle-grade polyester product is prepared through a solid phase device by adopting a common method to obtain the final product).
In this example, the amount of hot pot grade base polyester chip produced in-line was: 450 tons/day, the prepared polyester basic slice is detected, and the detection result is shown in table 1;
in this example, the amount of bottle grade based polyester chip obtained from the two-wire preparation was: 450 tons/day, then the prepared polyester base slice is detected, and the detection result is shown in the table 2.
Example 5
This example produced a product with a load of 600. The method comprises the following steps:
a second method for producing a plurality of polyester-like intermediates using the above-mentioned production system for a plurality of polyester-like intermediates, comprising the steps of:
(1) preparing required raw materials: pure Terephthalic Acid (PTA), isophthalic acid (IPA), ethylene glycol antimony, a reddish agent solution with the mass concentration of 160ppm, a bluish agent solution with the mass concentration of 800ppm, and diethylene glycol;
(2) adding Purified Terephthalic Acid (PTA), ethylene glycol antimony, 160ppm by mass of a red agent solution, 800ppm by mass of a blue agent solution and diethylene glycol into the raw materials prepared in the step (1), mixing and stirring the raw materials in a slurry preparation tank I, wherein the mass percentages of the components are as follows: PTA: 68-69%, ethylene glycol: 27-29%, ethylene glycol antimony: 1.2-1.3%, and a redness agent solution: 0.3-0.4%, bluing agent solution: 0.15 to 0.19%, diethylene glycol: 0.4-0.5%, and uniformly mixing and stirring;
and (2) adding the isophthalic acid (IPA) and the ethylene glycol prepared in the step (1) into a slurry preparation tank II, and mixing and stirring, wherein the slurry preparation tank II comprises the following components in percentage by mass: IPA: 50%, ethylene glycol: 50 percent, mixing and stirring evenly;
(3) uniformly stirring the mixture in the slurry preparation tank I and the slurry preparation tank II in the step (2);
discharging the mixture in the slurry preparation tank I from a discharge port at the lower end of the slurry preparation tank I, conveying the mixture to a slurry conveying pump through a material conveying pipeline, conveying the mixture to a first feed port of a first-stage esterification reaction kettle through a material conveying pipeline A under the action of the slurry conveying pump, and adding the mixture into the first-stage esterification reaction kettle; the flow rate of the mixture when the mixture is added into a first-stage esterification reaction kettle is 26000-30000 kg/h, the mixture is added and then reacted in the first-stage esterification reaction kettle, the temperature during the reaction is 256 +/-2 ℃, the pressure during the reaction is 60-70 KPa, and the reaction time is 4.5-5.5 hours, (the liquid level in the first-stage esterification reaction kettle is (65 +/-1)%), and the material of the first-stage esterification reaction is obtained after the reaction is finished;
(4) conveying the material obtained in the step (3) after the primary esterification reaction to a three-way pipe joint through a material conveying pipeline, and then respectively conveying the material to a material conveying pipeline branch pipe B and a material conveying pipeline branch pipe C through the three-way pipe joint;
the material of the first-stage esterification reaction in the material conveying pipeline branch pipe B is added into the first-stage second-stage esterification reaction kettle through a first feed inlet of the first-stage second-stage esterification reaction kettle to carry out the first-stage second-stage esterification reaction; in the process, the adding force of the materials of the first-stage esterification reaction in the material conveying pipeline branch pipe B added into the first-line second-stage esterification reaction kettle is 11000-13000 kg/h; after the addition, the temperature of reaction in a first-line secondary esterification reaction kettle is 258 +/-2 ℃, the pressure of the reaction is 3-8 KPa, the reaction time is 1.2-1.5 hours, (the liquid level in the first-line secondary esterification reaction kettle is (60 +/-1)%), and the first-line secondary esterification reaction material is obtained after the reaction is finished;
meanwhile, the material of the first-stage esterification reaction in the material conveying pipeline branch pipe C is added into the second-line second-stage esterification reaction kettle through a first feed port of the second-line second-stage esterification reaction kettle, and the mixture in the slurry preparation tank II is also added into the second-line second-stage esterification reaction kettle through a second feed port of the second-line second-stage esterification reaction kettle through a first slurry conveying pump and is mixed with the material of the first-stage esterification reaction for second-stage esterification reaction; in the process, when the materials of the first-order esterification reaction in the material conveying pipeline branch pipe C are added into the second-line second-order esterification reaction kettle through the first feed port of the second-line second-order esterification reaction kettle, the flow rate is 11000-13000 kg/h, and when the mixture in the slurry preparation tank II is added into the second-line second-order esterification reaction kettle through the second feed port of the second-line second-order esterification reaction kettle through the material conveying pipeline, the flow rate is 450-550 kg/h; after the addition is finished, carrying out reaction in a second-line secondary esterification reaction kettle, wherein the reaction temperature is 258 +/-2 ℃, the pressure is 3-8 KPa and the reaction time is 1.2-1.5 h, (the liquid level in the second-line secondary esterification reaction kettle is (60 +/-1)%); after the reaction is finished, a material of the second-line second-stage esterification reaction is obtained;
(5) discharging a material of the first-line second-stage esterification reaction obtained after the esterification reaction in the first-line second-stage esterification reaction kettle in the step (4) from a discharge port at the bottom of the reaction kettle, conveying the material to a first-line pre-polycondensation reactor through a material conveying pipeline for pre-polycondensation reaction, wherein the upper chamber temperature and the upper chamber pressure during the reaction in the first-line pre-polycondensation reactor are 268 +/-0.5 ℃ and 7-10 KPa (a), the lower chamber temperature and the lower chamber pressure are 271 +/-0.5 ℃ and 1.1-1.2 KPa (a), the reaction time is 2-2.5 hours, (the liquid level of the upper chamber is 25% and the liquid level of the lower chamber is 50% during the first-line second-stage pre-polycondensation reaction); conveying a first-line pre-polycondensation product obtained after the reaction to a first-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction, wherein the temperature and the pressure during the reaction in the first-line final polycondensation reactor are 278-285 ℃, 120-250 KPa (a), the reaction time is 1.5-2.5 hours, (the liquid level during the first-line final polycondensation reaction is (23 +/-2)%), and obtaining a hot tank grade basic polyester slice after the reaction is finished; (the basic slice of the hot tank grade polyester product is an intermediate of the hot tank grade polyester product, and the obtained basic slice of the hot tank grade polyester product is prepared by a common method through a solid phase device to obtain a final polyester product);
discharging a second-line second-stage esterification reaction material obtained after the esterification reaction in the second-line second-stage esterification reaction kettle in the step (4) from a discharge port at the bottom of the second-line second-stage esterification reaction kettle, conveying the second-line second-stage esterification reaction material to a second-line pre-polycondensation reactor for reaction through a material conveying pipeline, wherein the upper chamber temperature and the upper chamber pressure are 268 +/-0.5 ℃ and 7-10 KPa (a) respectively during the reaction in the second-line pre-polycondensation reactor, the lower chamber temperature and the lower chamber pressure are 271 +/-0.5 ℃ and 1.1-1.2 KPa (a) respectively during the reaction, and the reaction time is 2-2.5 hours, (the liquid level of the upper chamber is 25% and the liquid level of the lower chamber is 50% during the second-line second-stage; discharging the second-line pre-polycondensation product obtained after the reaction through a discharge port of a second-line pre-polycondensation reactor, conveying the second-line pre-polycondensation product to the second-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction, wherein the temperature during the final polycondensation reaction is 278-285 ℃, the reaction pressure is 120-250 KPa (a), and the reaction time is 1.5-2.5 hours, (the liquid level during the second-line final polycondensation reaction is (20 +/-2)%), obtaining a bottle-grade-based polyester slice after the reaction is finished, (the base slice of the bottle-grade polyester product is an intermediate of the bottle-grade polyester product, and the obtained base slice of the bottle-grade polyester product is prepared through a solid phase device by adopting a common method to obtain the final polyester product).
In this example, the amount of hot pot grade base polyester chip produced in-line was: 300 tons/day, the prepared polyester basic slice is detected, and the detection result is shown in table 1;
in this example, the amount of bottle grade based polyester chip obtained from the two-wire preparation was: 300 tons/day, then detecting the prepared polyester basic slice, wherein the detection result is shown in table 2;
TABLE 1 test results of base slices for preparing hot can grade polyester products in the above examples
TABLE 2 test results of the base chip for preparing bottle-grade polyester products in the above examples
Claims (10)
1. The device for producing the multiple types of polyester intermediates is characterized by comprising a slurry preparation tank I, wherein the slurry preparation tank I is connected with a slurry delivery pump through a material delivery pipeline, the slurry delivery pump is communicated with a feed inlet of a primary esterification reaction kettle through a material delivery pipeline A, a first discharge outlet of the primary esterification reaction kettle is communicated with a three-way pipe joint through a material delivery pipeline, and two material delivery pipeline branch pipes, namely a material delivery pipeline branch pipe B and a material delivery pipeline branch pipe C, are led out from the three-way pipe joint; the material conveying pipeline branch pipe B is communicated with a first feeding hole of the first-line second-stage esterification reaction kettle, a discharging hole of the first-line second-stage esterification reaction kettle is communicated with a feeding hole of the first-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the first-line pre-polycondensation reactor is communicated with a feeding hole of the first-line final-polycondensation reactor through a material conveying pipeline; the material conveying pipeline branch pipe C is communicated with a first feeding hole of the second-line second-stage esterification reaction kettle, a discharging hole of the second-line second-stage esterification reaction kettle is communicated with a feeding hole of the second-line pre-polycondensation reactor through a material conveying pipeline, and a discharging hole of the second-line pre-polycondensation reactor is communicated with a feeding hole of the second-line final polycondensation reactor through a material conveying pipeline;
the device also comprises a slurry preparation tank II, wherein the bottom of the slurry preparation tank II is provided with a first discharge hole and a second discharge hole; a first discharge hole at the bottom of the slurry preparation tank II is communicated with a first slurry conveying pump through a material conveying pipeline D, the first slurry conveying pump is communicated with a first flow regulating valve through a material conveying pipeline E, and the first flow regulating valve is communicated with a second feed hole of the first-line second-stage esterification reaction kettle through a material conveying pipeline F; and a second discharge port at the bottom of the slurry preparation tank II is communicated with a second slurry delivery pump through a material delivery pipeline M, the second slurry delivery pump is communicated with a second flow regulating valve through a material delivery pipeline N, and the second flow regulating valve is communicated with a second feed port of the second-line second-stage esterification reaction kettle through a material delivery pipeline P.
2. The production device of the various polyester intermediates according to claim 1, wherein a flow meter A and a three-way valve are arranged on the material conveying pipeline A, and the three-way valve is communicated with the feed inlet of the slurry preparation tank I through a return pipeline; and valves are arranged on the material conveying pipeline branch pipe B and the material conveying pipeline branch pipe C.
3. The production plant of various polyester intermediates according to claim 1, wherein said material transfer conduit D is provided with a three-way valve a, said three-way valve a being in communication with a glycol storage device via a first flush line; and the material conveying pipeline M is provided with a three-way valve b, and the three-way valve b is communicated with the ethylene glycol storage device through a second flushing pipeline.
4. The apparatus for producing the plurality of kinds of polyester intermediates according to claim 1, wherein the material transfer piping E is provided with a first check valve, a three-way valve c and a three-way valve E in this order; the material conveying pipeline N is sequentially provided with a second check valve, a three-way valve d and a three-way valve f; the three-way valve c is communicated with the three-way valve d through a material conveying pipeline S, and the three-way valve e is communicated with the three-way valve f through a material conveying pipeline T; the material conveying pipeline S is provided with a three-way valve g, the material conveying pipeline T is provided with a three-way valve h, and the three-way valve g and the three-way valve h are communicated through a material conveying pipeline Q.
5. The apparatus for producing the plurality of kinds of polyester intermediates according to claim 4, wherein a slurry flow meter and a valve are provided on said material conveying pipe Q.
6. The production device of the multiple types of polyester intermediates, as claimed in any one of claims 1 to 5, wherein the material conveying pipeline F is provided with a three-way valve j, the three-way valve j is communicated with the ethylene glycol storage device through a third flushing pipeline, and the three-way valve j is further communicated with the feed inlet of the slurry preparation tank II through a first return pipeline; and the material conveying pipeline P is provided with a three-way valve k, the three-way valve k is communicated with the ethylene glycol storage device through a fourth flushing pipeline, and the three-way valve k is communicated with a feeding hole of the slurry preparation tank II through a second backflow pipeline.
7. A method for producing a plurality of kinds of polyesters using the production apparatus for a plurality of kinds of polyester intermediates of claim 1, characterized by comprising the steps of:
(1) preparing the required raw materials of PTA, IPA, ethylene glycol, a catalyst, an erythroid solution, a blue agent solution and diethylene glycol;
(2) adding the material prepared in the step (1) into a slurry preparation tank I, and stirring, wherein the components and the mass percentages of the components in the slurry preparation tank I are as follows, PTA: 68-69%, ethylene glycol: 27-29%, catalyst: 1.2-1.3%, and a redness agent solution: 0.3-0.4%, bluing agent solution: 0.15 to 0.19%, diethylene glycol: 0.4-0.5% of the raw materials are mixed and stirred uniformly; simultaneously, IPA and glycol are added into the slurry preparation tank II and are uniformly stirred, the mass percent of IPA in the slurry preparation tank II is 50%, and the mass percent of glycol is 50%; the materials in the slurry preparation tank I and the slurry preparation tank II are uniformly mixed and stirred;
(3) after the mixture obtained in the step (2) is uniformly mixed and stirred, the mixture obtained in the slurry preparation tank I is conveyed to a slurry conveying pump from a discharge port at the lower end of the slurry stirring tank I through a material conveying pipeline, conveyed to a first feed port of the primary esterification reaction kettle through a material conveying pipeline A under the action of the conveying pump, and added into the primary esterification reaction kettle;
the flow rate of the materials in the slurry preparation tank I when the materials are added into the primary esterification reaction kettle is 26000-48000 kg/h; after the addition, the reaction temperature in a first-stage esterification reaction kettle is 250-265 ℃, the reaction time is 4-5.5 hours, and the reaction pressure is 60-70 KPa; after the first-stage esterification reaction is finished, obtaining a material of the first-stage esterification reaction;
(4) respectively conveying the materials of the primary esterification reaction obtained in the step (3) to a material conveying pipeline branch pipe B and a material conveying pipeline branch pipe C through a three-way pipe joint;
then the material of the first-stage esterification reaction is conveyed to a first feed inlet of the first-line second-stage esterification reaction kettle by a material conveying pipeline branch pipe B and added into the first-line second-stage esterification reaction kettle to carry out the second-stage esterification reaction; in the process, the flow of the material conveying pipeline branch pipe B conveyed into the first-line second-stage esterification reaction kettle is 11000-21000 kg/h; after the addition, the reaction time in the first-line second-stage esterification reaction kettle is 1.2-1.5 h, the reaction temperature is 255-270 ℃, and the reaction pressure is 3-8 KPa; after the reaction is finished, a first-line secondary esterification reaction material is obtained;
meanwhile, the material of the first-stage esterification reaction is conveyed to a first feed port of the second-line second-stage esterification reaction kettle through a material conveying pipeline branch pipe C and added into the second-line second-stage esterification reaction kettle, and meanwhile, the mixed material in the slurry configuration tank II is conveyed to a second feed port of the second-line second-stage esterification reaction kettle through a first slurry conveying pump and added into the second-line second-stage esterification reaction kettle, and is mixed with the material added from the first feed port to carry out second-stage esterification reaction; in the process, the flow of the material when the material is added into the first charging opening of the two-line two-stage esterification reaction kettle through the material conveying pipeline branch pipe C is as follows: 11000 to 21000kg/h, wherein the flow rate of the mixed material in the slurry preparation tank II when the mixed material is added through a second feed inlet of the second-line secondary esterification reaction kettle is 850 kg/h; after the materials are added, the reaction time in the second-line second-stage esterification reaction kettle is 1.2-1.5 h, the reaction temperature is 255-270 ℃, and the reaction pressure is 3-8 KPa; after the reaction is finished, a material of the second-line second-stage esterification reaction is obtained;
(5) discharging a material of the first-line second-stage esterification reaction obtained after the esterification reaction in the first-line second-stage esterification reaction kettle in the step (4) from a discharge hole at the bottom of the reaction kettle, conveying the material to a first-line pre-polycondensation reactor through a material conveying pipeline, and carrying out pre-polycondensation reaction; the reaction time of the pre-polycondensation reaction in the first-line pre-polycondensation reactor is 2-2.5 h, the upper chamber temperature of the reaction is 265-275 ℃, the lower chamber temperature is 270-276 ℃, the upper chamber pressure of the reaction is 7-10 KPa (a), and the lower chamber pressure is 1.1-1.2 KPa (a); discharging a pre-polycondensation product obtained after the pre-polycondensation reaction is finished through a discharge port of the pre-polycondensation reactor, and conveying the pre-polycondensation product to a first-line final polycondensation reactor through a material conveying pipeline for reaction final polycondensation; carrying out a final polycondensation reaction in a first-line final polycondensation reactor for 1.5-2.5 h, at a reaction temperature of 278-285 ℃ and a reaction pressure of 120-250 KPa (a), and obtaining a basic slice of a hot tank grade polyester product after the reaction is finished;
discharging a second-line second-stage esterification reaction material obtained after the esterification reaction in the second-line second-stage esterification reaction kettle in the step (4) from a discharge hole at the bottom of the second-line second-stage esterification reaction kettle, conveying the material to a second-line pre-polycondensation reactor through a material conveying pipeline, and reacting; the reaction time of the reaction in the second-line pre-polycondensation reactor is 2-2.5 h, the upper chamber temperature of the reaction is 265-275 ℃, the lower chamber temperature of the reaction is 270-276 ℃, the upper chamber pressure of the reaction is 7-10 KPa (a), the lower chamber pressure is 1.1-1.2 KPa (a), the pre-polycondensation product obtained after the second-line pre-polycondensation reaction is finished is discharged from a discharge port of the second-line pre-polycondensation reactor, and then is conveyed into the second-line final polycondensation reactor through a material conveying pipeline for final polycondensation reaction; the reaction time is 1.5-2.5 h, the reaction temperature is 278-285 ℃, the reaction pressure is 120-250 KPa (a) when the reaction is carried out in the second-line final polycondensation reactor, and the basic slice of the bottle-grade polyester product is obtained after the reaction is finished.
8. The method for producing polyesters according to claim 7, wherein the production plant for polyesters further comprises the steps of: and (4) after the material after the first-stage esterification reaction is conveyed to the first-line second-stage esterification reaction kettle through the material conveying pipeline branch pipe B, the mixture in the slurry preparation tank II is also added into the first-line second-stage esterification reaction kettle through the first slurry conveying pump to be mixed with the material after the first-stage esterification reaction for second-stage esterification reaction, and after the second-stage esterification reaction, pre-polycondensation and final polycondensation are sequentially carried out to obtain the basic slice of the bottle-grade polyester product.
9. The method for producing polyesters according to claim 7, wherein the production plant for polyesters further comprises the steps of: and (4) conveying the material subjected to the first-stage esterification reaction to a second-line second-stage esterification reaction kettle through a material conveying pipeline branch pipe C, then performing second-stage esterification reaction, after the second-stage esterification reaction is finished, sequentially conveying the material to a pre-polycondensation reactor and a final polycondensation reactor through a material conveying pipeline to perform pre-polycondensation and final polycondensation reaction, and after the final polycondensation reaction is finished, obtaining a basic slice of a hot pot-grade polyester product.
10. The process for producing polyesters using a production plant for polyesters intermediates as claimed in claim 7, wherein the catalyst in the step (1) is ethylene glycol antimony; the mass concentration of the redness agent in the redness agent solution is 160 PPM; the mass concentration of the blueness agent in the blueness agent solution is 800 PPM.
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| CN104262598A (en) * | 2014-10-14 | 2015-01-07 | 浙江万凯新材料有限公司 | Online polyester production conversion equipment and production conversion method adopting same |
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